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Continuous reaction method

A reaction and reaction kettle technology, applied in the field of chemistry, can solve the problems of low equipment capacity, low conversion rate, high energy consumption, etc., and achieve the effects of increasing production capacity, reducing manual operations, and improving energy utilization.

Active Publication Date: 2012-07-11
ZHEJIANG NHU CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] The above gap reactions have the following disadvantages: 1. Most of them are equilibrium reactions, and the conversion rate is not high; 2. Non-productive time such as feeding, heating, cooling, and discharging takes a large proportion of the total production time, and the production capacity of the unit equipment is small; 3. , Because it is an equilibrium reaction, it is necessary to remove a light component from the top of the tower to promote the reaction, resulting in a lot of energy consumption

Method used

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Examples

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Effect test

Embodiment 1

[0021] Synthesis of butyl ether : in such as figure 2 In the shown device, 300Kg of n-butanol and 1.2Kg of strongly acidic ion exchange resin catalyst are dropped into a 500L kettle. Open the jacketed steam for heating. When there is reflux at the top of the tower, reflux and divide water for 30 minutes at an internal temperature of 120-130°C. The vaporization amount is 80Kg / Hr, and the water is separated from the valve at the bottom of the water separator. After 30 minutes, turn off the jacket heating, turn on the circulation pump, turn on the scraped film evaporator, set the heating steam pressure of the scraped film evaporator to 0.35MPa, and set the feed flow rate to 120Kg / Hr. After the system is stable for 10 minutes, the output speed of n-butyl ether at the bottom of the wiped film evaporator will reach 30-40Kg / Hr. Prepare n-butanol in the raw material tank, switch operation, and feed continuously into the kettle with a feed flow rate of about 45Kg / Hr. At this time,...

Embodiment 2

[0025] Synthesis of isobutyl acetate: Pack 50Kg of supported solid acid catalyst at the bottom of the packing layer of the rectifying tower, and then fill with 4mBX packing. in such as figure 2 In the shown device, 210Kg of isobutanol, 150Kg of acetic acid, and 80Kg of cyclohexane are dropped into a 500L kettle. Open the jacketed steam for heating. When there is reflux at the top of the tower, reflux at an internal temperature of 110-115°C for water separation and reaction for 30 minutes. The vaporization amount is 100Kg / Hr, and the water is separated from the valve at the bottom of the water separator. After 30 minutes, turn off the jacket heating, turn on the circulation pump, turn on the scraped film evaporator, set the heating steam pressure of the scraped film evaporator to 0.22MPa, and set the feed flow rate to 135Kg / Hr. After the system is stable for 10 minutes, the discharge rate of isobutyl acetate at the bottom of the wiped film evaporator will reach 40-45Kg / Hr. ...

Embodiment 3

[0029] Synthesis of prenyl diprenol: in such as figure 2 In the shown device, 240Kg of prenol, 80Kg of prenal, 0.08Kg of hydrogen peroxide, and 80Kg of toluene were put into a 500L kettle. Open the vacuum valve on the condenser to control the system vacuum at -0.08MPa. Open the jacketed steam for heating. When there is reflux at the top of the tower, reflux and divide water for 30 minutes at an internal temperature of 80-100°C. The vaporization amount is 100Kg / Hr. It is a negative pressure operation, so a double valve is required to switch the water). After 30 minutes, turn off the jacket heating, turn on the circulation pump, turn on the wiped film evaporator, set the heating steam pressure of the wiped film evaporator to 0.30MPa, and set the feed flow rate to 120Kg / Hr. After the system is stable for 10 minutes, the acetal discharge rate at the bottom of the wiped film evaporator will reach 20-25Kg / Hr (because the whole system is operated under negative pressure, a liqui...

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Abstract

The invention discloses a continuous reaction method. The conventional intermittent reaction is almost balanced reaction, conversation rate is low, the proportion of nonproductive time in the total production time is small, and unit capacity of equipment is low. The continuous reaction method comprises the following steps of: feeding raw materials for reaction into a reaction kettle, feeding the raw materials flowing out of the bottom of the reaction kettle into reaction heating equipment, starting the reaction heating equipment and heating, feeding vapor and liquid mixture flowing out of the top of the reaction heating equipment into vapor-liquid separation equipment, feeding raw material vapor obtained from the top of the vapor-liquid separation equipment into a reaction kettle, wherein a rectifying column arranged on the reaction kettle is stably in a refluxing state, and feeding light components flowing out of the top of the rectifying column into a light component collection tank; and feeding liquid flowing out of the bottom of the vapor-liquid separation equipment into the reaction heating equipment again, and feeding liquid flowing out of the bottom of the reaction heating equipment into a product tank. Common intermittent reaction is improved to continuous reaction, and unit capacity of equipment is improved.

Description

technical field [0001] The present invention relates to chemical field, specifically a kind of method that carries out continuous reaction. Background technique [0002] Most of the reaction equipment used in etherification reaction, esterification reaction, aldol condensation reaction, aldehyde ketone condensation reaction, etc. are composed of reaction kettle, rectification tower, condenser, light component receiving tank, falling film evaporator, circulation pump, etc. Equipment composition, the usual reaction process is: put raw materials (including catalyst and water-carrying agent, etc.) The raw materials that have been reacted are recovered, cooled, and the desired product is obtained at the bottom of the still. [0003] The above gap reactions have the following disadvantages: 1. Most of them are equilibrium reactions, and the conversion rate is not high; 2. The non-productive time of feeding, heating, cooling, and discharging takes a large proportion of the total p...

Claims

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Application Information

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IPC IPC(8): C07B41/04C07B41/12C07C43/04C07C41/09C07C69/14C07C67/08C07C43/303C07C41/56
Inventor 张谦冯仪红
Owner ZHEJIANG NHU CO LTD
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